Integrated method for synthetising gasoline from methyl alcohol or dimethyl ether

An integrated method and technology of dimethyl ether, applied in the preparation of liquid hydrocarbon mixtures, petroleum industry, biological raw materials, etc., can solve the problems of high energy consumption and complicated process of the system

Active Publication Date: 2014-06-18
CHINA NAT OFFSHORE OIL CORP +2
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

Although the quality of methanol-to-gasoline products can be improved through this

Method used

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  • Integrated method for synthetising gasoline from methyl alcohol or dimethyl ether
  • Integrated method for synthetising gasoline from methyl alcohol or dimethyl ether

Examples

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Effect test

Embodiment 1

[0028] The raw material is refined methanol, the synthetic oil reactor is a fixed bed reactor, the reaction conditions are temperature 380°C, pressure 1.0MPa, methanol WHSV=1.0h -1 . The liquefied gas aromatization reactor adopts a fixed bed reactor, the reaction conditions are temperature 450°C, pressure 0.5MPa, raw material WHSV 1.0h -1 , the catalyst is a Ga / Ce-ZSM-5 molecular sieve catalyst, in which the Ga content is 1.5%, and the Ce content is 0.5%. The transalkylation reactor adopts a fixed bed reactor, the reaction conditions are temperature 300°C, pressure 1.2MPa, raw material WHSV 1.0h -1 , the catalyst is a Mo / Ni-Y molecular sieve catalyst, wherein the Mo content is 1.5%, and the Ni content is 1.0%. Under the above process conditions, the temperature of the discharge from the bottom of the E-5 flash tower is 130°C, and it can enter the E-15 fractionation tower after a simple heat exchange. After the materials are mixed, the temperature is 300°C, and they can ente...

Embodiment 2

[0030] The raw material is refined methanol, the synthetic oil reactor is a moving bed reactor, the reaction conditions are temperature 400°C, pressure 1.5MPa, methanol WHSV=1.5h -1 . The liquefied gas aromatization reactor adopts a moving bed reactor, the reaction conditions are temperature 500°C, pressure 0.2MPa, raw material WHSV 0.8h -1 , the catalyst is a Ga / Fe-ZSM-5 molecular sieve catalyst, in which the Ga content is 3.0%, and the Fe content is 2.0%. The transalkylation reactor adopts a fixed bed reactor, the reaction conditions are temperature 320°C, pressure 1.8MPa, raw material WHSV 0.7h -1 , the catalyst is a Mo / La-Y molecular sieve catalyst, wherein the Mo content is 3.0%, and the La content is 0.3%. Under the above process conditions, the discharge temperature of the bottom of the E-5 flash tower is 150°C, and it can enter the E-15 fractionation tower after a simple heat exchange. After mixing the materials, the temperature is 320°C, and can enter the E-16 tran...

Embodiment 3

[0032] The raw material is dimethyl ether, the synthetic oil reactor is a fluidized bed reactor, the reaction conditions are temperature 420°C, pressure 1.8MPa, methanol WHSV=2.0h -1 . The liquefied gas aromatization reactor adopts a fluidized bed reactor, the reaction conditions are temperature 550°C, pressure 0.2MPa, raw material WHSV 1.5h -1 , the catalyst is a Ga / Zn-ZSM-5 molecular sieve catalyst, in which the Ga content is 3.0%, and the Zn content is 1.0%. The transalkylation reactor adopts a fixed bed reactor, the reaction conditions are temperature 340°C, pressure 2.0MPa, raw material WHSV 1.2h -1 , the catalyst is a Mo / Co-Y molecular sieve catalyst, in which the Mo content is 3.0%, and the Co content is 2.0%. Under the above process conditions, the discharge temperature of the bottom of the E-5 flash tower is 170°C, and it can enter the E-15 fractionation tower after simple heat exchange. The product of the E-11 aromatization reactor and the bottom of the E-15 fracti...

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Abstract

The invention discloses an integrated method for synthetising gasoline from methyl alcohol or dimethyl ether. The integrated method is characterized by comprising the following steps: generating hydrocarbons rich in gasoline components from methyl alcohol or dimethyl ether in a synthesis reactor; separating through a flash tank, a gas-liquid separation tank and a fractionating tower to obtain C1-2 hydrocarbons, C3-4 hydrocarbons, light gasoline components, heavy gasoline components and water, wherein the light gasoline components are discharged as products; entering water into a sewage treatment unit; returning C1-2 hydrocarbons to the synthesis reactor after being supersized by a compressor; aromatizing the C3-4 hydrocarbons again, and then directly mixing the product with the heavy gasoline components to enter an alkyl transfer reactor as the raw material; returning the reaction product to the flash tower; discharging a little of C1-2 and heavy gasoline components as byproducts. The integrated method is simple in technological process, and the system is low in energy consumption; on the basis of fed refined methanol, the yield of the gasoline achieves 36-40%; on the basis of the fed dimethyl ether, the yield of the gasoline achieves 50-54%.

Description

technical field [0001] The invention belongs to the technical field of deep processing of methanol or dimethyl ether, and in particular relates to an integrated method for synthesizing gasoline from methanol or dimethyl ether. Background technique [0002] The methanol or dimethyl ether synthetic gasoline technology is developed on the basis of the conversion of methanol into aromatics on ZSM-5 molecular sieves developed by Mobil. The gasoline synthesized by this technology is sulfur-free, nitrogen-free, and has low olefin content. It can be used as The use of high-quality gasoline blending components is of great significance to our country. [0003] In recent years, driven by research related to coal-to-liquids, investment in domestic coal-based methanol installations has continued to increase, resulting in an increase in methanol production capacity year by year. By the end of 2012, the total domestic methanol production capacity had reached 52 million tons. However, the ...

Claims

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Application Information

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IPC IPC(8): C10G3/00
CPCY02P30/20
Inventor 王银斌于海斌臧甲忠郭春垒舒畅姜雪丹成宏南军汪洋李滨
Owner CHINA NAT OFFSHORE OIL CORP
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